EP2729601A1 - Réduction de dioxyde de carbone en acides carboxyliques, glycols, et carboxylates - Google Patents

Réduction de dioxyde de carbone en acides carboxyliques, glycols, et carboxylates

Info

Publication number
EP2729601A1
EP2729601A1 EP12808004.1A EP12808004A EP2729601A1 EP 2729601 A1 EP2729601 A1 EP 2729601A1 EP 12808004 A EP12808004 A EP 12808004A EP 2729601 A1 EP2729601 A1 EP 2729601A1
Authority
EP
European Patent Office
Prior art keywords
alloy
acid
carboxylic acid
compartment
carbon dioxide
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
EP12808004.1A
Other languages
German (de)
English (en)
Other versions
EP2729601A4 (fr
EP2729601B1 (fr
Inventor
Emily Barton Cole
Kyle Teamey
Andrew B. Bocarsly
Narayanappa Sivasankar
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Avantium Knowledge Centre BV
Original Assignee
Liquid Light Inc
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Liquid Light Inc filed Critical Liquid Light Inc
Publication of EP2729601A1 publication Critical patent/EP2729601A1/fr
Publication of EP2729601A4 publication Critical patent/EP2729601A4/fr
Application granted granted Critical
Publication of EP2729601B1 publication Critical patent/EP2729601B1/fr
Not-in-force legal-status Critical Current
Anticipated expiration legal-status Critical

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B3/00—Electrolytic production of organic compounds
    • C25B3/20—Processes
    • C25B3/25—Reduction
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B11/00—Electrodes; Manufacture thereof not otherwise provided for
    • C25B11/04—Electrodes; Manufacture thereof not otherwise provided for characterised by the material
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B1/00—Electrolytic production of inorganic compounds or non-metals
    • C25B1/50—Processes
    • C25B1/55—Photoelectrolysis
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B15/00—Operating or servicing cells
    • C25B15/08—Supplying or removing reactants or electrolytes; Regeneration of electrolytes
    • C25B15/085—Removing impurities
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B3/00—Electrolytic production of organic compounds
    • C25B3/01—Products
    • C25B3/07—Oxygen containing compounds
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B3/00—Electrolytic production of organic compounds
    • C25B3/20—Processes
    • C25B3/25—Reduction
    • C25B3/26—Reduction of carbon dioxide
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B9/00—Cells or assemblies of cells; Constructional parts of cells; Assemblies of constructional parts, e.g. electrode-diaphragm assemblies; Process-related cell features
    • C25B9/17—Cells comprising dimensionally-stable non-movable electrodes; Assemblies of constructional parts thereof
    • C25B9/19—Cells comprising dimensionally-stable non-movable electrodes; Assemblies of constructional parts thereof with diaphragms
    • C25B9/21—Cells comprising dimensionally-stable non-movable electrodes; Assemblies of constructional parts thereof with diaphragms two or more diaphragms

Definitions

  • the present disclosure generally relates to the field of electrochemical reactions, and more particularly to methods and /or systems for electrochemical production of carboxylic acids, glycols, and carboxylates from carbon dioxide.
  • a mechanism for mitigating emissions is to convert carbon dioxide into economically valuable materials such as fuels and industrial chemicals. If the carbon dioxide is converted using energy from renewable sources, both mitigation of carbon dioxide emissions and conversion of renewable energy into a chemical form that can be stored for later use may be possible.
  • the present invention is directed to using particular cathode materials, homogenous heterocyclic amine catalysts, and an electrolytic solution to reduce carbon dioxide to a carboxylic acid intermediate preferably including at least one of formic acid, glycolic acid, glyoxylic acid, oxalic acid, or lactic acid.
  • the carboxylic acid intermediate may be processed further to yield a glycol-based reaction product.
  • the present invention includes the process, system, and various components thereof.
  • FIGS. 1A and 1 B depict a block diagram of a preferred system in accordance with an embodiment of the present disclosure
  • FIG. 2 is a flow diagram of a preferred method of electrochemical production of a reaction product from carbon dioxide.
  • FIG. 3 is a flow diagram of another preferred method of electrochemical production of a reaction product from carbon dioxide.
  • an electrochemical system that converts carbon dioxide to carboxylic acid intermediates, carboxylic acids, and glycols.
  • Use of a homogenous heterocyclic catalyst facilitates the process.
  • the reduction of the carbon dioxide to produce carboxylic acid intermediates, carboxylic acids, and glycols may be preferably achieved in a divided electrochemical or photoelectrochemical cell having at least two compartments.
  • One compartment contains an anode suitable to oxidize water, and another compartment contains a working cathode electrode and a homogenous heterocyclic amine catalyst.
  • the compartments may be separated by a porous glass frit, microporous separator, ion exchange membrane, or other ion conducting bridge. Both compartments generally contain an aqueous solution of an electrolyte.
  • Carbon dioxide gas may be continuously bubbled through the cathodic electrolyte solution to preferably saturate the solution or the solution may be pre-saturated with carbon dioxide.
  • System 100 may be utilized for electrochemical production of carboxylic acid intermediates, carboxylic acids, and glycols from carbon dioxide and water (and hydrogen for glycol production).
  • the system (or apparatus) 100 generally comprises a cell (or container) 102, a liquid source 104 (preferably a water source, but may include an organic solvent source), an energy source 106, a gas source 108 (preferably a carbon dioxide source), a product extractor 1 10 and an oxygen extractor 1 12.
  • a product or product mixture may be output from the product extractor 1 10 after extraction.
  • An output gas containing oxygen may be output from the oxygen extractor 1 12 after extraction.
  • the cell 102 may be implemented as a divided cell.
  • the divided cell may be a divided electrochemical cell and /or a divided photochemical cell.
  • the cell 102 is generally operational to reduce carbon dioxide (C0 2 ) into products or product intermediates.
  • the cell 102 is operational to reduce carbon dioxide to carboxylic acid intermediates (including salts such as formate, glycolate, glyoxylate, oxalate, and lactate), carboxylic acids, and glycols.
  • the reduction generally takes place by introducing (e.g., bubbling) carbon dioxide into an electrolyte solution in the cell 102.
  • a cathode 120 in the cell 102 may reduce the carbon dioxide into a carboxylic acid or a carboxylic acid intermediate.
  • the production of a carboxylic acid or carboxylic acid intermediate may be dependent on the pH of the electrolyte solution, with lower pH ranges favoring carboxylic acid production.
  • the pH of the cathode compartment may be adjusted to favor production of one of a carboxylic acid or carboxylic acid intermediate over production of the other, such as by introducing an acid (e.g., HCl or H 2 S0 4 ) to the cathode compartment.
  • Hydrogen may be introduced to the carboxylic acid or carboxylic acid intermediate to produce a glycol or a carboxylic acid, respectively.
  • the hydrogen may be derived from natural gas or water.
  • the cell 102 generally comprises two or more compartments (or chambers) 1 14a- 1 14b, a separator (or membrane) 116, an anode 1 18, and a cathode 120.
  • the anode 118 may be disposed in a given compartment (e.g., 1 14a).
  • the cathode 120 may be disposed in another compartment (e.g., 1 14b) on an opposite side of the separator 116 as the anode 1 18.
  • the cathode 120 includes materials suitable for the reduction of carbon dioxide including cadmium, a cadmium alloy, cobalt, a cobalt alloy, nickel, a nickel alloy, chromium, a chromium alloy, indium, an indium alloy, iron, an iron alloy, copper, a copper alloy, lead, a lead alloy, palladium, a palladium alloy, platinum, a platinum alloy, molybdenum, a molybdenum alloy, tungsten, a tungsten alloy, niobium, a niobium alloy, silver, a silver alloy, tin, a tin alloy, rhodium, a rhodium alloy, ruthenium, a ruthenium alloy, carbon, and mixtures thereof.
  • materials suitable for the reduction of carbon dioxide including cadmium, a cadmium alloy, cobalt, a cobalt alloy, nickel, a nickel alloy, chromium, a chromium alloy
  • An electrolyte solution 122 may fill both compartments 1 14a-1 14b.
  • the aqueous solution 122 preferably includes water as a solvent and water soluble salts for providing various cations and anions in solution, however an organic solvent may also be utilized.
  • the organic solvent is present in an aqueous solution, whereas in other implementations the organic solvent is present in a non-aqueous solution.
  • the catholyte 122 may include sodium and/or potassium cations or a quaternary amine (preferably tetramethyl ammonium or tetraethyl ammonium).
  • the catholyte 122 may also include divalent cations (e.g., Ca 2+ , Mg 2+ , Zn 2+ ) or a divalent cation may be added to the catholyte solution.
  • a homogenous heterocyclic catalyst 124 is preferably added to the compartment 1 14b containing the cathode 120.
  • the homogenous heterocyclic catalyst 124 may include, for example, one or more of 4- hydroxy pyridine, adenine, a heterocyclic amine containing sulfur, a heterocyclic amine containing oxygen, an azole, a benzimidazole, a bipyridine, furan, an imidazole, an imidazole related species with at least one five-member ring, an indole, a lutidine, methylimidazole, an oxazole, phenanthroline, pterin, pteridine, a pyridine, a pyridine related species with at least one six-member ring, pyrrole, quinoline, or a thiazole, and mixtures thereof.
  • the homogenous heterocyclic catalyst 124 is preferably present in the compartment 114b at a concentration of between about 0.001 M and about 1M, and more preferably between about 0.01M and 0.5M.
  • the pH of the compartment 1 14b is preferably between about 1 and 8.
  • a pH range of between about 1 to about 4 is preferable for production of carboxylic acids from carbon dioxide.
  • a pH range of between about 4 to about 8 is preferable for production of carboxylic acid intermediates from carbon dioxide.
  • the liquid source 104 preferably includes a water source, such that the liquid source 104 may provide pure water to the cell 102.
  • the liquid source 104 may provide other fluids to the cell 102, including an organic solvent, such as methanol, acetonitrile, and dimethylfuran.
  • the liquid source 104 may also provide a mixture of an organic solvent and water to the cell 102.
  • the energy source 106 may include a variable voltage source.
  • the energy source 106 may be operational to generate an electrical potential between the anode 1 18 and the cathode 120.
  • the electrical potential may be a DC voltage.
  • the applied electrical potential is generally between about -1 .5V vs. SCE and about -4V vs. SCE, preferably from about -1 .5V vs. SCE to about -3V vs. SCE, and more preferably from about -1 .5 V vs. SCE to about -2.5V vs. SCE.
  • the gas source 108 preferably includes a carbon dioxide source, such that the gas source 108 may provide carbon dioxide to the cell 102.
  • the carbon dioxide is bubbled directly into the compartment 1 14b containing the cathode 120.
  • the compartment 1 14b may include a carbon dioxide input, such as a port 126a configured to be coupled between the carbon dioxide source and the cathode 120.
  • the carbon dioxide may be obtained from any source (e.g., an exhaust stream from fossil-fuel burning power or industrial plants, from geothermal or natural gas wells or the atmosphere itself).
  • the carbon dioxide may be obtained from concentrated point sources of generation prior to being released into the atmosphere.
  • high concentration carbon dioxide sources may frequently accompany natural gas in amounts of 5% to 50%, exist in flue gases of fossil fuel (e.g., coal, natural gas, oil, etc.) burning power plants, and high purity carbon dioxide may be exhausted from cement factories, from fermenters used for industrial fermentation of ethanol, and from the manufacture of fertilizers and refined oil products.
  • Certain geothermal steams may also contain significant amounts of carbon dioxide.
  • the carbon dioxide emissions from varied industries, including geothermal wells, may be captured on-site.
  • the capture and use of existing atmospheric carbon dioxide in accordance with some embodiments of the present invention generally allow the carbon dioxide to be a renewable and essentially unlimited source of carbon.
  • the product extractor 1 10 may include an organic product and/or inorganic product extractor.
  • the product extractor 1 10 generally facilitates extraction of one or more products (e.g., carboxylic acid, and /or carboxylic acid intermediate) from the electrolyte 122.
  • the extraction may occur via one or more of a solid sorbent, carbon dioxide- assisted solid sorbent, liquid-liquid extraction, nanofiltration, and electrodialysis.
  • the extracted products may be presented through a port 126b of the system 100 for subsequent storage, consumption, and/or processing by other devices and /or processes.
  • the carboxylic acid or carboxylic acid intermediate is continuously removed from the cell 102, where cell 102 operates on a continuous basis, such as through a continuous flow-single pass reactor where fresh catholyte and carbon dioxide is fed continuously as the input, and where the output from the reactor is continuously removed.
  • the carboxylic acid or carboxylic acid intermediate is continuously removed from the catholyte 122 via one or more of adsorbing with a solid sorbent, liquid-liquid extraction, and electrodialysis.
  • the separated carboxylic acid or carboxylic acid intermediate may be placed in contact with a hydrogen stream to produce a glycol or carboxylic acid, respectively. For instance, as shown in FIG.
  • the system 100 may include a secondary reactor 132 into which the separated carboxylic acid or carboxylic acid intermediate from the product extractor 1 10 and hydrogen stream from a hydrogen source 134 are introduced.
  • the secondary reactor 132 generally permits interaction between the separated carboxylic acid or carboxylic acid intermediate from the product extractor 110 and the hydrogen to produce a glycol or carboxylic acid, respectively.
  • the secondary reactor 132 may include reactor conditions that differ from ambient conditions.
  • the secondary reactor 132 preferably includes a temperature range and a pressure range that is higher than that of ambient conditions. For instance, a preferred temperature range of the secondary reactor 132 is between about 50°C and about 500°C, and a preferred pressure range of the secondary reactor 132 is between about 5 atm and 1000 atm.
  • the secondary reactor may include a solvent and a catalyst to facilitate the reaction between the separated carboxylic acid or carboxylic acid intermediate from the product extractor 1 10 and the hydrogen stream from the hydrogen source 134.
  • Preferred catalysts include Rh, Ru0 2 , Ru, Pt, Pd, Re, Cu, Ni, Co, Cu-Ni, and binary metals and /or metal oxides thereof.
  • the catalyst may be a supported catalyst, where the support may include Ti, Ti0 2 , or C.
  • Preferred solvents include aqueous and non-aqueous solvents, such as water, ether, and tetrahydrofuran.
  • the oxygen extractor 1 12 of FIG. 1A is generally operational to extract oxygen (e.g., 0 2 ) byproducts created by the reduction of the carbon dioxide and /or the oxidation of water.
  • the oxygen extractor 1 12 is a disengager/flash tank.
  • the extracted oxygen may be presented through a port 128 of the system 100 for subsequent storage and /or consumption by other devices and /or processes.
  • Chlorine and/or oxidatively evolved chemicals may also be byproducts in some configurations, such as in an embodiment of processes other than oxygen evolution occurring at the anode 118. Such processes may include chlorine evolution, oxidation of organics to other saleable products, waste water cleanup, and corrosion of a sacrificial anode. Any other excess gases (e.g., hydrogen) created by the reduction of the carbon dioxide and water may be vented from the cell 102 via a port 130.
  • the method (or process) 200 generally comprises a step (or block) 202, a step (or block) 204, a step (or block) 206, and a step (or block) 208.
  • the method 200 may be implemented using the system 100.
  • a liquid may be introduced to a first compartment of an electrochemical cell.
  • the first compartment may include an anode.
  • Introducing carbon dioxide to a second compartment of the electrochemical cell may be performed in the step 204.
  • the second compartment may include a solution of an electrolyte, a cathode, and a homogenous heterocyclic amine catalyst.
  • the cathode may be selected from the group consisting of cadmium, a cadmium alloy, cobalt, a cobalt alloy, nickel, a nickel alloy, chromium, a chromium alloy, indium, an indium alloy, iron, an iron alloy, copper, a copper alloy, lead, a lead alloy, palladium, a palladium alloy, platinum, a platinum alloy, molybdenum, a molybdenum alloy, tungsten, a tungsten alloy, niobium, a niobium alloy, silver, a silver alloy, tin, a tin alloy, rhodium, a rhodium alloy, ruthenium, a ruthenium alloy, carbon, and mixtures thereof.
  • an electric potential may be applied between the anode and the cathode in the electrochemical cell sufficient for the cathode to reduce the carbon dioxide to a carboxylic acid intermediate.
  • the production of the carboxylic acid intermediate is preferably controlled by selection of particular cathode materials, catalysts, pH ranges, and electrolytes, such as disclosed in U.S. Application No. 12/846,221 , the disclosure of which is incorporated by reference.
  • Contacting the carboxylic acid intermediate with hydrogen to produce a reaction product may be performed in the step 208.
  • the secondary reactor 132 may permit interaction /contact between the carboxylic acid intermediate and the hydrogen, where the conditions of the secondary reactor 132 may provide for production of particular reaction products. [0025] Referring to FIG.
  • the method (or process) 300 generally comprises a step (or block) 302, a step (or block) 304, a step (or block) 306, a step (or block) 308, a step (or block) 310, and a step (or block) 312.
  • the method 300 may be implemented using the system 100.
  • a liquid may be introduced to a first compartment of an electrochemical cell.
  • the first compartment may include an anode.
  • Introducing carbon dioxide to a second compartment of the electrochemical cell may be performed in the step 304.
  • the second compartment may include a solution of an electrolyte, a cathode, and a homogenous heterocyclic amine catalyst.
  • an electric potential may be applied between the anode and the cathode in the electrochemical cell sufficient for the cathode to reduce the carbon dioxide to at least a carboxylate.
  • Acidifying the carboxylate to convert the carboxylate into a carboxylic acid may be performed in the step 308.
  • the acidifying step may include introduction of an acid from a make-up acid source.
  • the carboxylic acid may be extracted.
  • Contacting the carboxylic acid with hydrogen to form a reaction product may be performed in the step 312.
  • the reaction product includes one or more of formaldehyde, methanol, glycolic acid, glyoxal, glyoxylic aid, glycolaldehyde, ethylene glycol, acetic acid, acetaldehyde, ethanol, propylene glycol, or isopropanol.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Electrochemistry (AREA)
  • Materials Engineering (AREA)
  • Metallurgy (AREA)
  • Inorganic Chemistry (AREA)
  • Electrolytic Production Of Non-Metals, Compounds, Apparatuses Therefor (AREA)

Abstract

La présente invention concerne des procédés et systèmes pour la conversion électrochimique de dioxyde de carbone en acides carboxyliques, glycols, et carboxylates. Un procédé peut comprendre, entre autres, les étapes (A) à (D) suivantes. L'étape (A) peut introduire de l'eau dans un premier compartiment d'une cellule électrochimique. Le premier compartiment peut comporter une anode. L'étape (B) peut introduire du dioxyde de carbone dans un second compartiment de la cellule électrochimique. Le second compartiment peut comporter une solution d'un électrolyte et une cathode. L'étape (C) peut appliquer un potentiel électrique entre l'anode et la cathode dans la cellule électrochimique suffisant pour réduire le dioxyde de carbone en un intermédiaire d'acide carboxylique. L'étape (D) peut mettre en contact l'intermédiaire d'acide carboxylique avec de l'hydrogène pour produire un produit réactionnel.
EP12808004.1A 2011-07-06 2012-07-05 Réduction de dioxyde de carbone en acide oxalique, et hydration de celui-ci Not-in-force EP2729601B1 (fr)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
US201161504848P 2011-07-06 2011-07-06
PCT/US2012/045578 WO2013006711A1 (fr) 2011-07-06 2012-07-05 Réduction de dioxyde de carbone en acides carboxyliques, glycols, et carboxylates
US13/542,152 US8592633B2 (en) 2010-07-29 2012-07-05 Reduction of carbon dioxide to carboxylic acids, glycols, and carboxylates

Publications (3)

Publication Number Publication Date
EP2729601A1 true EP2729601A1 (fr) 2014-05-14
EP2729601A4 EP2729601A4 (fr) 2014-12-31
EP2729601B1 EP2729601B1 (fr) 2018-05-09

Family

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Family Applications (1)

Application Number Title Priority Date Filing Date
EP12808004.1A Not-in-force EP2729601B1 (fr) 2011-07-06 2012-07-05 Réduction de dioxyde de carbone en acide oxalique, et hydration de celui-ci

Country Status (9)

Country Link
US (2) US8592633B2 (fr)
EP (1) EP2729601B1 (fr)
JP (1) JP2014518335A (fr)
KR (1) KR20140050038A (fr)
CN (1) CN103649374A (fr)
AU (1) AU2012278949A1 (fr)
BR (1) BR112014000052A2 (fr)
CA (1) CA2841062A1 (fr)
WO (1) WO2013006711A1 (fr)

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CA2841062A1 (fr) 2013-01-10
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EP2729601B1 (fr) 2018-05-09
US8592633B2 (en) 2013-11-26
AU2012278949A1 (en) 2014-01-16
US20140027303A1 (en) 2014-01-30
US20120277465A1 (en) 2012-11-01
CN103649374A (zh) 2014-03-19
KR20140050038A (ko) 2014-04-28
JP2014518335A (ja) 2014-07-28

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